Entrained-flow gasifier and gasification method using the same for synthesizing syngas from biomass fuel

ABSTRACT

A method for gasifying biomass using a gasifier, the gasifier including a furnace body and a fuel pretreatment system. The method includes 1) crushing and sieving a biomass fuel to yield particle size-qualified fuel particles, 2) exciting working gas to yield plasma, and spraying the plasma into the gasifier, 3) spraying the particle size-qualified fuel particles into the gasifier via nozzles, synchronously spraying an oxidizer via an oxygen/vapor inlet into the gasifier, and 4) monitoring the temperature and components of the syngas, regulating an oxygen flow rate, a vapor flow rate, and microwave power to maintain the process parameters within a preset range and to control a temperature of the syngas to be between 900 and 1200° C., collecting the syngas from the syngas outlet at the top of the furnace body, and discharging liquid slag from the slag outlet.

CROSS-REFERENCE TO RELATED APPLICATIONS

This application is a divisional of and claims domestic prioritybenefits to U.S. application Ser. No. 14/314,023, filed Jun. 24, 2014,now pending. U.S. application Ser. No. 14/314,023, filed Jun. 24, 2014,now pending, is a continuation-in-part of International PatentApplication No. PCT/CN2012/083562 with an international filing date ofOct. 26, 2012, designating the United States, now pending, and furtherclaims priority benefits to Chinese Patent Application No.201110449413.4 filed Dec. 29, 2011. The contents of all of theaforementioned applications, including any intervening amendmentsthereto, are incorporated herein by reference. Inquiries from the publicto applicants or assignees concerning this document or the relatedapplications should be directed to: Matthias Scholl P. C., Attn.: Dr.Matthias Scholl Esq., 245 First Street, 18^(th) Floor, Cambridge, Mass.02142.

BACKGROUND OF THE INVENTION

Field of the Invention

The invention relates to the gasification of biomass, and moreparticularly to an entrained-flow gasifier and a gasification methodusing the same for synthesizing syngas from biomass fuel in the presenceof microwave-excited plasma.

Description of the Related Art

Biomass gasification process generally includes fixed bed gasification,fluidized bed gasification, entrained flow gasification. The fixed bedgasification has defects such as low gasification temperature, high tarcontent, and low-quality syngas. The fluidized bed gasification has amoderate gasification temperature and convenient feeding anddischarging, to ensure the stable fluidization, the furnace temperaturemust be controlled to be moderate. Low gasification temperature resultsin high content of tar in the syngas. The tar is difficult to remove andeasily blocks and corrodes the valves, pipes, and auxiliary equipment.The removal of the tar costs much. The entrained flow gasification has ahigh and uniform reaction temperature, high gasification efficiency, andthe tar is completely cracked. However, the entrained flow gasificationhas a high requirement on the particle size of the raw materials. Ingeneral, the particle size should be less than 0.1 mm Biomass containsmuch cellulose, which is very difficult to be crushed to have a smallparticle size to meet the requirement of the entrained flow bed. Thesmaller the required particle size is, the larger the abrasion of thecrusher is, and the higher the energy consumption is. Large particlesize causes the low carbon conversion rate and low cold gas efficiency,which greatly limits the application of conventional entrained flow bedsin the synthesis of syngas.

SUMMARY OF THE INVENTION

In view of the above-described problems, it is one objective of theinvention to provide an entrained-flow gasifier and a gasificationmethod using the same for synthesizing syngas of carbon monoxide andhydrogen from biomass fuel in the presence of microwave-excited plasmawith characteristics of economy, high efficiency, and feasibility.

To achieve the above objective, in accordance with one embodiment of theinvention, there is provided a microwave plasma based entrained flowgasifier of biomass, comprises a furnace body and a fuel pretreatmentsystem. The furnace body is vertically disposed and comprises a fuelinlet disposed at a lower part of the furnace body, a syngas outletdisposed at a top of the furnace body, and a slag outlet disposed at abottom of the furnace body. The fuel inlet presents in the form ofnozzles. The fuel pretreatment system is disposed outside of the furnacebody, and comprises a fuel crushing apparatus, a sieving apparatusdisposed downstream to the fuel crushing apparatus, a first fuelcontainer for receiving particle size-qualified fuel, a second fuelcontainer for receiving particle size-unqualified fuel, and a feedinghopper disposed downstream to the first fuel container. The first fuelcontainer and the second fuel container are disposed side-by-sidedownstream to the sieving apparatus; a bottom of the feeding hopper isconnected to the furnace body via the nozzles. A monitoring unit isdisposed close to the syngas outlet at the top of the furnace body. Thenozzles are disposed radially along the furnace body and are between 2and 4 in number. One or two layers of microwave plasma generators are inparallel disposed at a gasification zone of the furnace body, and eachlayer of the microwave plasma generator comprises between 2 and 4working gas inlets.

In a class of this embodiment, the microwave plasma generators aredisposed horizontally/tangentially on the furnace body so as to prolongthe retention time of the melting particles of the biomass in the plasmaatmosphere.

In a class of this embodiment, the microwave plasma generators havelarge electrode gap, strong plasma activity, and wide volume range.

In a class of this embodiment, a microwave power source of the microwaveplasma generators has a basic frequency of 2.45 GHz, and a power of asingle microwave plasma generator is within 200 kW.

A method for gasifying biomass using the entrained flow gasifiercomprises:

-   -   1) crushing and sieving a biomass fuel using the fuel        pretreatment system to yield particle size-qualified fuel        particles, and transporting the particle size-qualified fuel        particles to the feeding hopper for use;    -   2) introducing working gas from the working gas inlets into the        microwave plasma generator, exciting the working gas to yield        high temperature, high degree of ionization, and high activity        of plasma, and spraying the plasma to into the gasifier;    -   3) spraying the particle size-qualified fuel particles into the        gasifier via the nozzles, synchronously spraying an oxidizer via        an oxygen/vapor inlet into the gasifier, so that a high        temperature and rapid thermal chemical reaction between the fuel        particles and the oxidizer in the presence of high activity of        plasma proceeds to yield syngas comprising carbon monoxide and        hydrogen; and    -   4) monitoring the temperature and components of the syngas,        regulating oxygen flow rate, vapor flow rate, and microwave        power to maintain the process parameters within a preset range,        collecting the syngas having a temperature of between 900 and        1200° C. from the syngas outlet at the top of the furnace body,        and discharging liquid slags from the slag outlet.

In a class of this embodiment, in step 1), the particle size-qualifiedfuel particles are received by the first fuel container, the particlesize-unqualified fuel particles are first received by the second fuelcontainer and then returned to the fuel pretreatment system for crushingagain until meeting the particle size requirement; the particlesize-qualified fuel particles are transported from the first containerto the feeding hopper; and the particle size of the fuel particles isbetween 0 and 5 mm.

In a class of this embodiment, in step 2), the start-up of the microwaveplasma generators is between 2 and 3 seconds earlier than the start-upof the nozzles of the gasifier; the working gas comprises an auxiliaryoxidizer, and is introduced into the microwave plasma generators via theworking gas inlets to be excited to yield high temperature, high degreeof ionization, and high activity of plasma.

In a class of this embodiment, in step 3), the particle size-qualifiedfuel particles are carried by carrier gas and sprayed into the gasifiervia the nozzles; the oxidizers are synchronously sprayed into thegasifier via the oxygen/vapor inlet, so that a partialoxidation-reduction reaction and high temperature gasification reactionbetween the fuel particles and the oxidizer proceed to yield syngascomprising a large amount of carbon monoxide and hydrogen and a smallamount of CO₂, CH₄, H₂S, and COS.

The syngas flows upward to the gasification zone of the microwave plasmagenerators, and mixes with the horizontally/tangentially sprayed plasmagas for high-temperature thermo-chemical gasification reaction atbetween 1200 and 1800° C., a central zone temperature is between 1800and 2000° C., a retention time of the syngas in the gasification zone isbetween 1 and 10 seconds, and the power of the microwave plasmagenerators is controlled to drive the reaction to proceed completely.

In step 4), the volume content of CO and H₂ in the syngas exceeds 85%,the syngas contains no tar and no phenolic compounds, the liquid slagdischarged from the slag outlet is chilled to be pollution-free, whichcan be used as a thermal insulation material.

In a class of this embodiment, in steps 2) and 3), the working gas andthe carrier gas are air and/or oxygen and/or vapor; and the vapor isoriginated from the recycling of sensible heat of high temperaturesyngas.

In this disclosure, the microwave plasma generator is disposed in thegasification zone of the gasifier. The working gas in the microwaveplasma generator is excited by microwave to produce plasma. Themicrowave-excited plasma is rich in oxidizers and has characteristics ofhigh temperature, high degree of ionization, high dispersity, and highactivity. When the working gas is sprayed into the redox zone of theentrained flow bed, in the presence of the high temperature and highactivity of plasma, on one hand, the reaction temperature is enhanced,which accelerates the chemical reaction, on the other hand, the hightemperature and high activity of plasma can greatly improve the chemicalreaction between syngas and solid-phase/liquid-phase biomass particles,thereby improving the heat and mass transfer rate, and shortening thechemical reaction time of the biomass fuel. The fuel conversion issignificantly improved within the same retention time. Compared to coal,the biomass fuel has large void space, high activity and low meltingpoint. Thus, in the presence of the high temperature and high activityof plasma, the particle size of the applied biomass fuel can besignificantly higher than that required by conventional entrained flowbed, and the conversion effect is ideal.

Additionally, the microwave plasma generator supplies an auxiliaryoxidizer for the gasification reaction, which ensures the balance anduniformity of the supply of the reactants, and inputs a certain thermalpower, which provides some external thermal source. The introduction ofthe auxiliary oxidizer is a good means to regulate the operation of thegasifier.

Advantages according to embodiments of the invention are summarized asfollows.

1. The biomass fuel has high activity, in the presence of hightemperature microwave-excited plasma, the carbon conversion rate reachesabout 99%, the cold gas efficiency exceeds 85%, and the activecomponents of CO and H₂ have high content.

2. The resulting syngas from the entrained flow gasifier contains no tarand no phenolic compounds, and the subsequent collection of the syngasis convenient.

3. In this disclosure, the biomass fuels do not need to be crushed tohave an extremely small particle sizes, that is to say, the applicationrange of the particle sizes of the biomass fuel is wide, and thus thegasifier has good economic efficiency.

4. The material feeding and the slag discharging are easy, and thegasification intensity is high, which facilitates the popularization.

BRIEF DESCRIPTION OF THE DRAWINGS

The invention is described hereinbelow with reference to accompanyingdrawings, in which:

FIG. 1 shows a schematic diagram of a microwave plasma based entrainedflow gasifier of biomass and a flow chart of a gasification method usingthe same according to one embodiment of the invention; and

FIG. 2 is a sectional view taken from Line A-A of FIG. 1.

In the drawings, the following reference numbers are used: 1. Fuelcrushing apparatus; 2. Sieving apparatus; 3. First fuel container forreceiving particle size-qualified fuel; 4. Second fuel container forparticle size-unqualified fuel; 5. Feeding hopper; 6. Nozzle; 7.Microwave plasma generator; 8. Gasifier; 9. Syngas outlet; 10. Slagoutlet; 11. Working gas inlet; 12. Monitoring unit; 13. Oxygen/vaporinlet.

DETAILED DESCRIPTION OF THE EMBODIMENTS

For further illustrating the invention, experiments detailing anentrained-flow gasifier and a gasification method using the same forsynthesizing syngas from biomass fuel are described below. It should benoted that the following examples are intended to describe and not tolimit the invention.

As shown in FIGS. 1 and 2, a microwave plasma based entrained flowgasifier 8 of biomass, comprises a cylindrical furnace body and a fuelpretreatment system. The furnace body is vertically disposed, andcomprises a fuel inlet disposed at a lower part of the furnace body, asyngas outlet 9 disposed at a top of the furnace body, and a slag outlet10 disposed at a bottom of the furnace body. The fuel inlet presents inthe form of nozzles 6. The fuel pretreatment system is disposed outsideof the furnace body, and comprises a fuel crushing apparatus 1, asieving apparatus 2 disposed downstream to the fuel crushing apparatus1, a first fuel container 3 for receiving particle size-qualified fuel,a second fuel container 4 for receiving particle size-unqualified fuel,and a feeding hopper 5 disposed downstream to the first fuel container.The first fuel container and the second fuel container are disposedside-by-side downstream to the sieving apparatus. A bottom of thefeeding hopper 5 is connected to the furnace body via the nozzles 6. Oneor two layers of microwave plasma generators 7 are in parallel disposedat a gasification zone of the furnace body for expanding the plasmareaction zone, and each layer of the microwave plasma generatorcomprises between 2 and 4 working gas inlets 11 (it is three in FIG. 2).The furnace body of the gasifier is cylindrical, or a combination ofcone and cylinder.

The positioning of the microwave plasma generators greatly affects thegasification of the biomass fuel. In this example, the microwave plasmagenerators 7 are disposed on the furnace body both horizontally andtangentially. Thus, the gas flow is fully burbled so as to prolong theretention time of the melting particles of the biomass in the plasmaatmosphere.

A monitoring unit 12 is disposed close to the syngas outlet 9 at the topof the furnace body to monitor the temperature and components of thesyngas, so as to regulate oxygen flow rate, vapor flow rate, andmicrowave power to maintain the process parameters within a presetrange.

The nozzles 6 are disposed radially along the furnace body and arebetween 2 and 4 in number. As needed, the number of the nozzles can beincreased or decreased.

The microwave plasma generators have large electrode gap, strong plasmaactivity, and wide volume range.

The microwave power source of the microwave plasma generators has abasic frequency of 2.45 GHz, and a power of a single microwave plasmagenerator is within 200 kW.

A method for gasifying biomass using the entrained flow gasifiercomprises:

1) Crushing and sieving a biomass fuel using the fuel crushing apparatus1 and the sieving apparatus 2 to yield particle size-qualified fuelparticles.

Specifically, the biomass fuel is crushed by the fuel crushing apparatusof the fuel pretreatment system to have appropriate particle sizes. Theparticle size of the biomass fuel is one of the key factors affectingthe gasification process. The smaller the required particle size is, thelarger the abrasion of the crusher is, and the higher the energyconsumption is. Large particle size causes the low carbon conversionrate and low cooled coal gas efficiency. The crushed biomass fuel istransported to the sieving apparatus 2. Through sieving, the particlesize-qualified fuel particles are received by the first fuel container3, and the particle size-unqualified fuel particles are first receivedby the second fuel container 4 and then returned to the fuelpretreatment system for crushing again until meeting the particle sizerequirement. Take rice hull as an example, the particle size of ricehull is between 7 and 10 mm in length, and 2 mm in width. The rice hulljust needs to be roughly crushed to have the particle size of between 1and 5 mm. Twigs and straw have a large original particle size, which canbe first crushed by a disc or drum crusher to have a particle size ofbetween 50 and 100 mm, and then be crushed by a hammer mill to have aparticle size of between 1 and 5 mm.

2) Introducing working gas from the working gas inlets 11 into themicrowave plasma generator 7, exciting the working gas to yield hightemperature, high degree of ionization, and high activity of plasma, andspraying the plasma to into the gasifier 8.

Specifically, the start-up of the microwave plasma generators 7 isbetween 2 and 3 seconds earlier than the start-up of the nozzles 6 ofthe gasifier. The working gas comprises an auxiliary oxidizer, and isintroduced into the microwave plasma generators 7 via the working gasinlets 11 to be excited to yield high temperature, high degree ofionization, and high activity of plasma, which is further sprayed intothe gasifier 8.

3) Spraying the particle size-qualified fuel particles into the gasifier8 via the nozzles 6, synchronously spraying an oxidizer via anoxygen/vapor inlet 13 into the gasifier, so that a high temperature andrapid thermal chemical reaction between the fuel particles and theoxidizer in the presence of high activity of plasma proceeds to yieldsyngas comprising a large amount of carbon monoxide and hydrogen and asmall amount of CO₂, CH₄, H₂S, and COS.

Specifically, the particle size-qualified fuel particles are transportedfrom the first container 3 to the feeding hopper 5. Thereafter, the fuelparticles are transported to the nozzles 6 of the furnace body from thebottom of the feeding hopper with the help of a gasifying agent and thenenter the gasifier 8 via the nozzles 6. The oxidizers are synchronouslysprayed into the gasifier via the oxygen/vapor inlet, so that a partialoxidation-reduction reaction and high temperature gasification reactionbetween the fuel particles and the oxidizer proceed to yield syngascomprising a large amount of carbon monoxide and hydrogen and a smallamount of CO₂, CH₄, H₂S, and COS.

The syngas flows upward to the gasification zone of the microwave plasmagenerators, and mixes with the horizontally/tangentially sprayed plasmagas for high-temperature thermo-chemical gasification reaction atbetween 1200 and 1800° C., a central zone temperature is between 1800and 2000° C., a retention time of the syngas in the gasification zone isbetween 1 and 10 seconds, and the power of the microwave plasmagenerators is controlled to drive the reaction to proceed completely.The syngas is finally collected from the syngas outlet 9 disposed at thetop of the gasifier. The volume content of CO and H₂ in the syngasexceeds 85%. The syngas contains no tar and no phenolic compounds. Theliquid slag discharged from the slag outlet 9 is chilled to bepollution-free, which can be used as a thermal insulation material. Thevapor is originated from the recycling of the high temperature syngas.

4) Monitoring the temperature and components of the syngas, regulatingoxygen flow rate, vapor flow rate, and microwave power to maintain theprocess parameters within a preset range, collecting the syngas having atemperature of between 900 and 1200° C. from the syngas outlet 9 at thetop of the furnace body, and discharging liquid slags from the slagoutlet 10.

In step 1), the particle size of the fuel particles is between 0 and 5mm, particularly about 2 mm.

In steps 2) and 3), the working gas and the carrier gas are air and/oroxygen and/or vapor; and the vapor is originated from the recycling ofsensible heat of high temperature syngas.

To achieve the optimal working conditions and satisfy the overallperformance requirement of the gasification, the key is to control thetemperature of the entrained flow bed, and to regulate the oxygen flowrate, vapor flow rate, and microwave power. The monitoring unit disposedclose to the syngas outlet can monitor the above parameters in realtime, thereby controlling the gasification process by chain and by fullautomation and maintaining the operation stability of the gasifier.

While particular embodiments of the invention have been shown anddescribed, it will be obvious to those skilled in the art that changesand modifications may be made without departing from the invention inits broader aspects, and therefore, the aim in the appended claims is tocover all such changes and modifications as fall within the true spiritand scope of the invention.

The invention claimed is:
 1. A method for gasifying biomass using agasifier, the gasifier comprising a furnace body comprising a fuelinlet, a syngas outlet and a slag outlet, the fuel inlet comprisingnozzles; and a fuel pretreatment system comprising a feeding hopper;wherein: the furnace body is vertically disposed; the fuel inlet isdisposed at a lower part of the furnace body; the syngas outlet isdisposed at a top of the furnace body; the slag outlet is disposed at abottom of the furnace body; the fuel pretreatment system is disposedoutside of the furnace body; a bottom of the feeding hopper is connectedto the furnace body via the nozzles; the nozzles are disposed radiallyalong the furnace body; and one or two layers of microwave plasmagenerators are disposed in parallel at a gasification zone of thefurnace body and each layer of the microwave plasma generators comprisesworking gas inlets; the method comprising: 1) crushing and sieving abiomass fuel using the fuel pretreatment system to yield particlesize-qualified fuel particles, and transporting the particlesize-qualified fuel particles to the feeding hopper; 2) introducingworking gas from the working gas inlets into the microwave plasmagenerator, exciting the working gas to yield high temperature, highdegree of ionization, and high activity of plasma, and spraying theplasma to into the gasifier; 3) spraying the particle size-qualifiedfuel particles into the gasifier via the nozzles, synchronously sprayingan oxidizer via an oxygen/vapor inlet into the gasifier, so that athermal-chemical reaction between the fuel particles and the oxidizer inthe presence of high activity of plasma proceeds to yield syngascomprising carbon monoxide and hydrogen; and 4) monitoring thetemperature and components of the syngas, regulating oxygen flow rate,vapor flow rate, and microwave power to maintain the process parameterswithin a preset range, collecting the syngas having a temperature ofbetween 900 and 1200° C. from the syngas outlet at the top of thefurnace body, and discharging liquid slags from the slag outlet.
 2. Themethod of claim 1, wherein the fuel pretreatment system furthercomprises a fuel crushing apparatus, a sieving apparatus, a first fuelcontainer for receiving the particle size-qualified fuel particles, anda second fuel container for receiving particle size-unqualified fuelparticles; a number of nozzles is between 2 and 4; a number of workinggas inlets is between 2 and 4; the sieving apparatus is disposeddownstream to the fuel crushing apparatus; the feeding hopper isdisposed downstream to the first fuel container; the first fuelcontainer and the second fuel container are disposed side-by-sidedownstream to the sieving apparatus; and a monitoring unit is disposedclose to the syngas outlet at the top of the furnace body.
 3. The methodof claim 1, wherein the fuel pretreatment system further comprises afuel crushing apparatus, a sieving apparatus disposed downstream to thefuel crushing apparatus, a first fuel container for receiving theparticle size-qualified fuel particles, and a second fuel container forreceiving particle size-unqualified fuel particles; the first fuelcontainer and the second fuel container are disposed side-by-sidedownstream to the sieving apparatus; and in step 1), the particlesize-qualified fuel particles are received by the first fuel container,the particle size-unqualified fuel particles are first received by thesecond fuel container and then returned to the fuel pretreatment systemfor crushing again until meeting the particle size requirement; theparticle size-qualified fuel particles are transported from the firstcontainer to the feeding hopper; and the particle size of the fuelparticles is less than 5 mm.
 4. The method of claim 1, wherein in step2), the start-up of the microwave plasma generators is between 2 and 3seconds earlier than the start-up of the nozzles of the gasifier; theworking gas comprises an auxiliary oxidizer, and is introduced into themicrowave plasma generators via the working gas inlets to be excited toyield high temperature, high degree of ionization, and high activity ofplasma.
 5. The method of claim 3, wherein in step 2), the start-up ofthe microwave plasma generators is between 2 and 3 seconds earlier thanthe start-up of the nozzles of the gasifier; the working gas comprisesan auxiliary oxidizer, and is introduced into the microwave plasmagenerators via the working gas inlets to be excited to yield hightemperature, high degree of ionization, and high activity of plasma. 6.The method of claim 4, wherein in step 3), the particle size-qualifiedfuel particles are carried by carrier gas and sprayed into the gasifiervia the nozzles; the oxidizers are synchronously sprayed into thegasifier via the oxygen/vapor inlet, so that a partialoxidation-reduction reaction and gasification reaction between the fuelparticles and the oxidizer proceed to yield syngas comprising a largeamount of carbon monoxide and hydrogen and a small amount of CO₂, CH₄,H₂S, and COS; the syngas flows upward to the gasification zone of themicrowave plasma generators, and mixes with thehorizontally/tangentially sprayed plasma gas for thermo-chemicalgasification reaction at between 1200 and 1800° C., a central zonetemperature is between 1800 and 2000° C., a retention time of the syngasin the gasification zone is between 1 and 10 seconds, and the power ofthe microwave plasma generators is controlled to drive the reaction toproceed completely.
 7. The method of claim 5, wherein in step 3), theparticle size-qualified fuel particles are carried by carrier gas andsprayed into the gasifier via the nozzles; the oxidizers aresynchronously sprayed into the gasifier via the oxygen/vapor inlet, sothat a partial oxidation-reduction reaction and gasification reactionbetween the fuel particles and the oxidizer proceed to yield syngascomprising a large amount of carbon monoxide and hydrogen and a smallamount of CO₂, CH₄, H₂S, and COS; the syngas flows upward to thegasification zone of the microwave plasma generators, and mixes with thehorizontally/tangentially sprayed plasma gas for thermo-chemicalgasification reaction at between 1200 and 1800° C., a central zonetemperature is between 1800 and 2000° C., a retention time of the syngasin the gasification zone is between 1 and 10 seconds, and the power ofthe microwave plasma generators is controlled to drive the reaction toproceed completely.
 8. The method of claim 1, wherein in step 4), thevolume content of CO and H₂ in the syngas exceeds 85%, the syngascontains no tar and no phenolic compounds, the liquid slag dischargedfrom the slag outlet is chilled to be pollution-free, which can be usedas a thermal insulation material.
 9. The method of claim 3, wherein instep 4), the volume content of CO and H₂ in the syngas exceeds 85%, thesyngas contains no tar and no phenolic compounds, the liquid slagdischarged from the slag outlet is chilled to be pollution-free, whichcan be used as a thermal insulation material.
 10. The method of claim 7,wherein in step 4), the volume content of CO and H₂ in the syngasexceeds 85%, the syngas contains no tar and no phenolic compounds, theliquid slag discharged from the slag outlet is chilled to bepollution-free, which can be used as a thermal insulation material. 11.The method of claim 8, wherein in steps 2) and 3), the working gas andthe carrier gas are air and/or oxygen and/or vapor; and the vapor isoriginated from the recycling of sensible heat of syngas.
 12. The methodof claim 9, wherein in steps 2) and 3), the working gas and the carriergas are air and/or oxygen and/or vapor; and the vapor is originated fromthe recycling of sensible heat of syngas.
 13. The method of claim 10,wherein in steps 2) and 3), the working gas and the carrier gas are airand/or oxygen and/or vapor; and the vapor is originated from therecycling of sensible heat of syngas.